US3406011A - Process for the manufacture of hydroxylammonium salts - Google Patents

Process for the manufacture of hydroxylammonium salts Download PDF

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Publication number
US3406011A
US3406011A US602157A US60215766A US3406011A US 3406011 A US3406011 A US 3406011A US 602157 A US602157 A US 602157A US 60215766 A US60215766 A US 60215766A US 3406011 A US3406011 A US 3406011A
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United States
Prior art keywords
catalyst
oxygen
reaction
acid
selectivity
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Expired - Lifetime
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US602157A
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English (en)
Inventor
Zirngibl Hans
Dornemann Alexander
Gerken Rudolf
Heine Heinz
Meyer Horst
Weise Johannes
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Bayer AG
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Bayer AG
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/082—Compounds containing nitrogen and non-metals and optionally metals
    • C01B21/14—Hydroxylamine; Salts thereof
    • C01B21/1409—Preparation
    • C01B21/1418—Preparation by catalytic reduction of nitrogen oxides or nitrates with hydrogen

Definitions

  • This invention relates to a process for the production of hydroxyl-ammonium salts.
  • a process for the production of hydroxyl-ammonium salts from nitric oxide and hydrogen in the presence of noble metal catalysts at tmeperatures of from 0 C. to 80 C. has now been found, in which the catalyst is periodically or continuously treated with oxygen for a time suificient to reactivate the catalyst to the desired activity and selectivity. It was surprisingly found that "ice the activity and selectivity of the noble metal catalysts can be kept approximately at a constant value over avery long period of time by a periodic or continuous intermediate treatment with oxygen.
  • the treatment can take place both in aqueous and in acid solution.
  • As the acid it is advantageous to use the sulphuric acid which is preferably also in the reaction of NC with hydrogen.
  • the treatment can be carried out at temperatures between 0 C. and C. and it is advantageous to work at temperatures of from 30 C. to 50 C.
  • treating with oxygen is meant contacting the noble metal catalyst, preferably for from 2 to 60 minutes, with oxygen itself or with an agent containing free oxygen, e.g., air or one which easily decomposes to form oxygen, e.g., peroxidic compounds such as hydrogen peroxide, ammonium peroxide disulfate, perborates, and the like or permanganate compounds such as potassium permanganate.
  • oxygen itself or with an agent containing free oxygen, e.g., air or one which easily decomposes to form oxygen, e.g., peroxidic compounds such as hydrogen peroxide, ammonium peroxide disulfate, perborates, and the like or permanganate compounds such as potassium permanganate.
  • the treatment of the catalyst occurs either in the reaction medium or after separation of the catalyst and resuspending in water or acid solution by bringing the catalyst continuously or periodically into intimate contact with oxygen.
  • Another possibility of maintaining the activity and selectivity of the catalyst according to the present invention is the continuous admixture of oxygen with the reaction gases in amounts of 0.01 to 1.0% by volume, preferably of 0.05 to 0.2% by volume, based on the amount of NO used.
  • the treatment of the catalyst when performed periodically, normally occurs after the neutralization of the reaction mixture by the reaction gases in such cases where the reaction is conducted batchwise.
  • the nitric oxide-hydrogen mixture in the reaction vessel is displaced by nitrogen and thereafter the catalyst is gased with oxygen or air, the amount of oxygen or the duration of gasing depending on the state of activity of the catalyst.
  • the introduction of the NO/H mixture is periodically interrupted. Thereafter the reaction vessel is flushed with nitrogen prior to the feeding in of oxygen or air. Thereafter the air or oxygen is replaced by nitrogen, whereupon the synthesis is continued.
  • the concurrent addition of oxygen or air to the synthesis gas for maintaining the activity and selectivity of the catalyst at an optimum level can be accomplished in the continuous as well as in the batchwise production of hydroxylamine.
  • the production of the hydroxylamine salts is carried out as known per se by introducing nitrogen oxide and hydrogen in an aqueous mineral acid solution containing the suspended catalyst therein.
  • the synthesis gas is fed into the acid catalyst mixture until the acid is nearly consumed, whereby preferably a pH of 2.5 is not exceeded, to avoid the formation of substantial amounts of ammonium or ammonium salts.
  • the hydroxyl-ammonium salts so obtained are, after removing the catalyst, either precipitated by cooling the reaction solution or the reaction solution with the hydroxylamine a 3 a a salt contained therein is directly used for synthesis, e.g., the production of lactams.
  • the salts can also be used as reducing agents, as photographic developers, as stabilizers, etc.
  • the reaction temperature is between and 80 C., preferably the reaction is carried out at a temperature of between 40 and 60 C.
  • concentration of free acid should amount to between 0.01 and 5.0 N; the molar ratio of NOzH is normally to be maintained at a range of between 1:15 and 1:3.0, preferably of between 1: 1.6 and 1:2.0.
  • the reaction is performed at normal pressure, however, it is possible to apply superpressure also.
  • acids the strong mineral acids such as sulfuric acid, hydrochloric acid, phosphoric acid, nitric acid or the like are used.
  • the metals of the platinum series and advantageously platinum itself may be used as noble metal catalysts.
  • Activated carbon or graphite can be employed as an acid resistant support material for the noble metals. It is known that activated carbon, used as a support material, has a better activity and selectivity than graphite. However, activated carbon has the disadvantage that with increasing use, the particles disintegrate to form smaller particles which increase the filtration time necessary to remove the catalyst and thus there are serious time losses caused by the filtering off of the reaction solution, which is periodically necessary.
  • catalysts the support materials of which consist of a mixture of activated carbon and graphite.
  • the preferred support materials consist of from about to 50% by weight activated carbon and 50 to 90% by weight graphite, advantageously about of activated carbon and 80% of graphite.
  • Such supports have a very high and constant selectivity and activity, without the rate of filtration increasing substantially as the period of use increases.
  • the catalysts to be used are preparedin the'usual manner, for example, by introducing activated carbon and graphite into dilute HCl, treating the suspension with hexachloroplatinic acid, heating the suspension to, for example, 70 C. and adding, for example, formic acid.
  • This catalyst comprising a mixed support of graphite and activated carbon, can be reactivated by contacting with oxygen inthe manner described above.
  • the catalyst according to the invention shows a surprisingly constant activity and selectivity while at the same time not substantially increasing filtration rates.
  • the present application are defined as follows: by activity, is meant the percentage of the N0 precipitated in the hydroxylammoniu'm salt and ammonium salt, related to the total quantity of NO introduced; the selectivity is defined as 100 times the ratio of mols of hydroxylammonium salt formed to the sum of the mols of hydroxylammonium salt and ammonium salt formed.
  • Example 1 Prior art
  • Example 2 (According to the invention) Up to the separation of catalyst and solution, the procedure was in accordance with Example 1. The catalyst after separation was washed with H 0 and suspended in 500 ml. of H 0. After adding approximately 10 anl. of 3% H 0 the solution was left at about 40 C. for approximately 15 minutes while stirring vigorously, and then 500 ml. of approximately 40% H SO were added. Gasification was once again carried out. The process was repeated more than 30 times and finally stopped without it, being possible to detect any deterioration in the overall result.
  • Example 2 No. of Total Selec- No. 01 Total Selecthroughconversion, tivlty throughconversion, tivity put I percent put percent
  • Example 3 parts of (F.T.) in minutes are indicated in TABLE 2-Continued Catalyst (a) Catalyst (b) Catalyst (c) N o. of throughput Sel. F.T. Act. Sel. FT. Act. Sel. F.T.
  • Example 6 catalysts Whereas only a slight superiority over the comparison Example 6 catalysts is found upto the 48th throughput of the mixed support catalyst, its superiority becomes clearly apparent with increasing age. For example, with the 184th throughput, the filtration time is increased to not quite four times by comparison with the graphite carrier catalyst; the activated carbon catalyst could no longer be used even after the 82nd throughput, because of filtration difiiculties.
  • Example 4 25 g. of a Pt/C catalyst are suspended in 1 litre of an approximately 20% H 80 and gasified at 40 C., while vigorously stirring with a NO/H mixture with a constant change of about 10 litres of NO per hour.
  • Example 1 In accordance with Example 4, an agitator vessel was charged with the catalyst and operated in the same manner for throughputs. In the case of the 10th throughput, the NO/H mixture was replaced by nitrogen. Thereafter within 10 minutes 3 litres of air were fed in. After flushing with nitrogen, the catalyst was separated from the reaction solution, resuspended in fresh acid and gasified again with NO/H The reactivation with air was repeated during the first 100 throughputs after every 10th run, thereafter the reactivation occurred after every 5th run. The results of expermirnents 4 and 5 have been set out in the following Table 3.
  • Example 5 N O conver- No conversion to Selectivity sion to Selectivity NH2OH+NH3 (percent) N HeoH-l-NHa (percent) (percent) (percent) A stirring vessel, as described in Example 4, additionally equipped with a filter unit, was charged with 25 g. of a Pt/ C catalyst and 1 litre of the sulphuric acid. At a temperature of 40 C., the suspension was gasified with 10 litres of NO and 18 litres of H per hour. After 9.5 hours, the acid was neutralized to a normality of 0.3 by the hydroxylarnine and ammonia formed. The
  • Example 7 The reaction was carried out in accordance with Example 6 with the exception that the aeration was performed continuously. 0.05% by volume of oxygen, based on the NO amount used was added to the synthesis gas. The experiment was interrupted after 2,000 hours without the occurrence of any reduction of the conversion. The activity and selectivity of the catalyst remained unchanged throughout the experiment.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US602157A 1965-12-28 1966-12-16 Process for the manufacture of hydroxylammonium salts Expired - Lifetime US3406011A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DEF0048021 1965-12-28
DEF0050788 1966-11-28

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US3406011A true US3406011A (en) 1968-10-15

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US (1) US3406011A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
BE (1) BE691894A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
CH (1) CH483363A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
DE (2) DE1567513B2 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
FR (1) FR1506859A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
GB (2) GB1179119A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
NL (1) NL6618291A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3663166A (en) * 1967-05-13 1972-05-16 Bayer Ag Platinum catalyst for the production of hydroxylamine
US3856924A (en) * 1971-01-02 1974-12-24 Basf Ag Production of hydroxylammonium nitrate
US3996161A (en) * 1974-03-05 1976-12-07 Chia Tung Yu Active carbon and a method of preparing the same
US4028274A (en) * 1976-06-01 1977-06-07 United Technologies Corporation Support material for a noble metal catalyst and method for making the same
US4054687A (en) * 1976-06-01 1977-10-18 United Technologies Corporation Method for making a fuel cell electrode
US4159309A (en) * 1977-03-30 1979-06-26 Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung Process for the catalytic reduction of reducible compounds in solution
US4457906A (en) * 1981-07-31 1984-07-03 Basf Aktiengesellschaft Preparation of hydroxylammonium salts
US4889704A (en) * 1987-04-24 1989-12-26 Basf Aktiengesellschaft Preparation of hydroxylammonium salts
US4895711A (en) * 1988-03-22 1990-01-23 Basf Aktiengesellschaft Preparation of hydroxylammonium salts

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4132800A1 (de) * 1991-10-02 1993-04-08 Basf Ag Verfahren zur herstellung von hydroxylammoniumsulfat
RU2287481C1 (ru) * 2005-09-27 2006-11-20 Открытое акционерное общество "КуйбышевАзот" (ОАО "КуйбышевАзот") Способ получения гидроксиламинсульфата
RU2287482C1 (ru) * 2005-09-27 2006-11-20 Открытое акционерное общество "КуйбышевАзот"(ОАО "КуйбышевАзот") Способ получения гидроксиламинсульфата
RU2305657C1 (ru) * 2006-01-10 2007-09-10 Открытое акционерное общество "КуйбышевАзот" (ОАО "КуйбышевАзот" Способ управления процессом получения гидроксиламинсульфата
RU2327633C2 (ru) * 2006-07-19 2008-06-27 Открытое акционерное общество "КуйбышевАзот" Способ получения гидроксиламинсульфата

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2626246A (en) * 1949-01-29 1953-01-20 Texas Co Regenerating cobalt catalysts by oxidation
US3133790A (en) * 1960-08-04 1964-05-19 Basf Ag Production of hydroxyl ammonium salts
US3295925A (en) * 1962-07-13 1967-01-03 Inventa Ag Process for the production of hydroxylamine

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2626246A (en) * 1949-01-29 1953-01-20 Texas Co Regenerating cobalt catalysts by oxidation
US3133790A (en) * 1960-08-04 1964-05-19 Basf Ag Production of hydroxyl ammonium salts
US3295925A (en) * 1962-07-13 1967-01-03 Inventa Ag Process for the production of hydroxylamine

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3663166A (en) * 1967-05-13 1972-05-16 Bayer Ag Platinum catalyst for the production of hydroxylamine
US3856924A (en) * 1971-01-02 1974-12-24 Basf Ag Production of hydroxylammonium nitrate
US3996161A (en) * 1974-03-05 1976-12-07 Chia Tung Yu Active carbon and a method of preparing the same
US4028274A (en) * 1976-06-01 1977-06-07 United Technologies Corporation Support material for a noble metal catalyst and method for making the same
US4054687A (en) * 1976-06-01 1977-10-18 United Technologies Corporation Method for making a fuel cell electrode
DE2719659A1 (de) * 1976-06-01 1977-12-15 United Technologies Corp Traegermaterial fuer einen edelmetallkatalysator, verfahren zur herstellung desselben und dessen verwendung
US4159309A (en) * 1977-03-30 1979-06-26 Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung Process for the catalytic reduction of reducible compounds in solution
US4457906A (en) * 1981-07-31 1984-07-03 Basf Aktiengesellschaft Preparation of hydroxylammonium salts
US4889704A (en) * 1987-04-24 1989-12-26 Basf Aktiengesellschaft Preparation of hydroxylammonium salts
US4895711A (en) * 1988-03-22 1990-01-23 Basf Aktiengesellschaft Preparation of hydroxylammonium salts

Also Published As

Publication number Publication date
FR1506859A (fr) 1967-12-22
GB1179120A (en) 1970-01-28
GB1179119A (en) 1970-01-28
CH483363A (de) 1969-12-31
BE691894A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html) 1967-06-28
NL6618291A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html) 1967-06-29
DE1567532A1 (de) 1970-08-20
DE1567513B2 (de) 1975-05-28
DE1567513A1 (de) 1970-04-16
DE1567532B2 (de) 1975-06-19

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